CN202030720U - Offshore natural gas liquefaction device - Google Patents
Offshore natural gas liquefaction device Download PDFInfo
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- CN202030720U CN202030720U CN2011200190563U CN201120019056U CN202030720U CN 202030720 U CN202030720 U CN 202030720U CN 2011200190563 U CN2011200190563 U CN 2011200190563U CN 201120019056 U CN201120019056 U CN 201120019056U CN 202030720 U CN202030720 U CN 202030720U
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Abstract
The utility model relates to an offshore natural gas liquefaction device, which comprises the following steps: 1) natural gas extracted from the seabed is fed to a heat-exchange fridge after pre-treatment; 2) carbon dioxide gas pre-arranged in a carbon dioxide pre-cooling circulation system enters the heat-exchange fridge after constant pressurization and cooling; 3) nitrogen pre-arranged in a double nitrogen expansion cooling circulation system is compressed into high-pressure nitrogen, the high-pressure nitrogen enters the heat-exchange fridge and is divided into two paths after carbon dioxide pre-cooling, one path of the high-pressure nitrogen is directly depressurized and cooled through a nitrogen expansion machine, the other path of the high-pressure nitrogen is depressurized and cooled through another nitrogen expansion machine after continuous pre-cooling, and the two paths of the low-pressure nitrogen flow back to the heat-exchange fridge for heat-exchange warming and are pressurized and cooled before returning to the heat-exchange fridge; and 4) the pre-treated natural gas enters a heavy hydrocarbon separation unit after pre-cooled by the carbon dioxide gas in the heat-exchange fridge, the natural gas is gradually cooled by the returned nitrogen and goes through cooling and the throttling cooling of a throttling valve after heavy hydrocarbon removal through gas-liquid separators and a rectifying tower, and liquid enters a storage tank for storage and gas is exhausted from a buffering tank for collection after gas-liquid mixture enters the buffering tank.
Description
Technical field
The utility model relates to the production equipment of a kind of natural gas liquids (LNG, Liquefied Natural Gas), particularly about a kind of marine natural gas liquefaction device.
Background technology
China's coastal waters natural gas source is abundant, total geological resource amount is about 5.9 tcms, but, these natural gas sources disperse, be distributed in basin, the mouth of the Zhujiang River, Yinggehai Basin ground, basin, the fine jade southeast, EAST CHINA SEA CONTINENTAL SHELF basin and basin, Bohai Sea Gulf, and wherein quite a few is gas field, deep-sea, marginal little gas field and low taste natural gas source.For these sources of the gas, if adopt modes such as traditional ocean stationary platform or submerged pipeline, exploitation then can can't be dropped into because of cost or technical limitation in most gas fields.
If adopt LNG-FPSO (Liquefied Natural Gas-Floating Production Storage﹠amp; Offloading, natural gas liquids Floating Production storage handler), can be according to the production status flexible configuration of marine natural-gas field, natural gas liquids aboard ship, be transported to the point of destination again, have and be convenient to migration, reusable, production efficiency advantages of higher, this is to promoting China's especially gas field, deep-sea, small-sized gas field development of marine site, and it is significant to make full use of hydrocarbon resources.As one of core of LNG-FPSO, the design of liquefying plant will produce very big influence to capital construction cost, working cost, serviceability and the security of engineering, but not occur being applied at present the liquefying plant of LNG-FPSO as yet.
Summary of the invention
At the problems referred to above, the purpose of this utility model provides the marine natural gas liquefaction device of a kind of LNG-FPSO of being applied to.
For achieving the above object, the utility model is taked following technical scheme: a kind of marine natural gas liquefaction device, it is characterized in that: it comprises a heat exchange ice chest, No. two heat exchange ice chests, No. three heat exchange ice chests and No. four heat exchange ice chests, the one cover carbon dioxide precooling recycle system, a cover dinitrogen gas swell refrigeration recycle system and a natural qi exhaustion heavy hydrocarbon of cover and a liquefaction system; The described carbon dioxide precooling recycle system comprises carbon dioxide compressor, water cooler and the carbonic acid gas throttling valve that connects a described heat exchange ice chest successively, and the output terminal of described carbonic acid gas throttling valve connects a described heat exchange ice chest; The described dinitrogen gas swell refrigeration recycle system comprises the nitrogen splitter that is connected with a described heat exchange ice chest, described nitrogen splitter output terminal is divided into two pipelines: a pipeline directly connects the nitrogen expansion machine, described nitrogen expansion machine connects a decompressor supercharging blower, and the output terminal of described nitrogen expansion machine connects described No. three heat exchange ice chests, No. two heat exchange ice chests and a heat exchange ice chest successively; Another pipeline be connected in series successively described No. two heat exchange ice chests, No. three heat exchange ice chests and another nitrogen expansion machine, this described nitrogen expansion machine also connects a decompressor supercharging blower, and the output terminal of this described nitrogen expansion machine connects described No. four heat exchange ice chests, No. three heat exchange ice chests, No. two heat exchange ice chests and a heat exchange ice chest successively; The input terminus of two described decompressor supercharging blowers all connects a described heat exchange ice chest, and output terminal all be connected in series successively water cooler, nitrogen compressor, water cooler, mixing tank connect a described heat exchange ice chest at last; Described natural qi exhaustion heavy hydrocarbon and liquefaction system comprise the primary separator that is connected with a described heat exchange ice chest, the output terminal of described primary separator is divided into two pipelines, article one, pipeline directly connects the rectifying tower middle part, and another connects described rectifying tower top by described No. two heat exchange ice chests, second-stage separators successively; The top of described rectifying tower is connected described No. three heat exchange ice chests, No. four heat exchange ice chests, Sweet natural gas throttling valve and LNG surge tanks with described second-stage separator successively by a mixing tank, and the output terminal of described LNG surge tank connects the LNG storage tank; The bottom of described rectifying tower be connected in series successively throttling valve, water cooler and LPG surge tank, the output terminal of described LPG surge tank connects the LPG storage tank.
The utility model is owing to take above technical scheme, it has the following advantages: 1, the utility model is owing to adopt carbonic acid gas to carry out precooling, adopt the dinitrogen swell refrigeration to be used for deep cooling and natural gas liquids, the heavy hydrocarbon separating unit has made full use of the cold in the liquefaction process and has realized that heavy hydrocarbon separates, and has reduced the load of pretreatment unit; The cooling of seawater direct current has improved operational efficiency, processing power and the seaworthiness of device, is applicable to that preferably the LNG of ocean environment produces.2, the water cooler of the utility model setting all adopts the cooled with seawater circulation, therefore, has advantages such as the water intaking temperature is low, aboundresources, has reduced the power consumption of compressor.3, two kinds of refrigeration agents that adopt in the utility model: nitrogen and carbonic acid gas, all belong to non-flammable gas, and low price, help reducing production costs, increase the security of device, wherein, nitrogen can be produced by nitrogen gas generator, do not need to store, the safe distance between each system can suitably shorten, and reduces floor space.4, the utility model is in the refrigeration cycle process, nitrogen is in gas phase all the time, is subjected to the influence of ship motion hardly, though there is gas-liquid two-phase in circulate carbon dioxide in the precooling, but as pure component, it is smaller that its gas-liquid separation process is subjected to the influence that hull rocks.5, the utility model and be the unitary system cryogen because the device valve member is few, equipment is few, has reduced the start time of a lot of utility appliance, does not need operations such as refrigeration agent proportioning, and control is simple and drive, stop rapid.6, the utility model is owing to adopted carbonic acid gas as the precooling circulating refrigerant, can effectively utilize carbonic acid gas vaporization latent heat, reduce the energy consumption of flow process, it is relatively poor to have solved the marine suitability of existing liquefaction technology preferably, reaches defectives such as conventional nitrogen expansion liquefying plant processing power is little, efficient is low.The utility model is insensitive to conditions such as the composition of Sweet natural gas, temperature, pressure, all meet the requirements than technical indicators such as power consumption, liquefied fractions, and whole device can carry out the modularization setting, facility compact, is convenient to install, and can be widely used in the marine gas extraction liquefaction process.
Description of drawings
Fig. 1 is the utility model structural representation
Fig. 2 is the utility model heat exchange ice chest module diagram
Fig. 3 is the utility model heavy hydrocarbon separation module synoptic diagram
Fig. 4 is the utility model hydrodynamic force module synoptic diagram
Fig. 5 is the utility model product stock module diagram
Embodiment
Below in conjunction with drawings and Examples the utility model is described in detail.
The utility model device comprises four heat exchange ice chests, 10,20,30,40, the one cover carbon dioxide precooling recycle systems 50, a cover dinitrogen gas swell refrigeration recycle system 60, a natural qi exhaustion heavy hydrocarbon of cover and liquefaction system 70 and some the liquefaction pipelines that connect successively.
As shown in Figure 1, the carbon dioxide precooling recycle system 50 comprises the carbon dioxide compressor 501 that connects heat exchange ice chest 10, the output terminal of carbon dioxide compressor 501 connects water cooler 502, carbon dioxide compressor 503, water cooler 504 and carbonic acid gas throttling valve 505 successively, and the output terminal of carbonic acid gas throttling valve 505 connects heat exchange ice chest 10.
The carbon dioxide precooling recycle system 50 utilizes the carbonic acid gas throttling to produce cold, enters heat exchange ice chest 10 and realizes the precooling effect.The workflow of the carbon dioxide precooling recycle system 50 is: the carbon dioxide that presets in the carbon dioxide precooling recycle system 50 passes through the two stages of compression of carbon dioxide compressor 501 and carbon dioxide compressor 503 successively to 6MPa, correspondence is cooled to 20 ℃ by water cooler 502 and water cooler 504 after each grade compression, at this moment, carbonic acid gas all liquefies, liquid carbon dioxide is depressurized to 0.6MPa through carbonic acid gas throttling valve 505, temperature is reduced to-52 ℃, this moment, carbonic acid gas was a gas-liquid two-phase, entering heat exchange ice chest 10 is used for precooling and enters Sweet natural gas in the heat exchange ice chest 10 and the nitrogen gas refrigerant in the heat exchange ice chest 10, after heat exchange heats up, proceed above-mentioned circulation process.
The dinitrogen gas swell refrigeration recycle system 60 comprises the nitrogen splitter 601 that is connected with heat exchange ice chest 10, nitrogen splitter 601 output terminals are divided into two pipelines, article one, pipeline directly connects nitrogen expansion machine 602, nitrogen expansion machine 602 connects decompressor supercharging blower 603, and the output terminal of nitrogen expansion machine 602 connects heat exchange ice chest 30, heat exchange ice chest 20 and heat exchange ice chest 10 successively; The input terminus of decompressor supercharging blower 603 connects heat exchange ice chest 10, and output terminal be connected in series successively water cooler 604, nitrogen compressor 605, water cooler 606, nitrogen compressor 607, water cooler 608 connect heat exchange ice chests 10 by mixing tank 609 at last.Another pipeline of nitrogen splitter 601 output terminals be connected in series successively heat exchange ice chest 20, heat exchange ice chest 30 and nitrogen expansion machine 610, nitrogen expansion machine 610 connects decompressor supercharging blower 611, and the output terminal of nitrogen expansion machine 610 connects heat exchange ice chest 40, heat exchange ice chest 30, heat exchange ice chest 20 and heat exchange ice chest 10 successively; The input terminus of decompressor supercharging blower 611 connects heat exchange ice chest 10, and output terminal be connected in series successively water cooler 612, nitrogen compressor 613, water cooler 614, nitrogen compressor 615, water cooler 616 connect heat exchange ice chests 10 by mixing tank 609 at last.
The workflow of the dinitrogen gas swell refrigeration recycle system 60 is:
The nitrogen that presets in the dinitrogen gas swell refrigeration recycle system 60, compressed to 8MPa, become high pressure nitrogen, high pressure nitrogen enters heat exchange ice chest 10, after-50 ℃, be divided into two strands by the carbon dioxide precooling in the carbon dioxide precooling recycle system 50 through nitrogen splitter 601:
One nitrogen of telling through nitrogen splitter 601 directly expands through nitrogen expansion machine 602, and to decompressor supercharging blower 603 output mechanical works, pressure is reduced to 2MPa, temperature is reduced to-115 ℃, enter heat exchange ice chest 30, heat exchange ice chest 20 then successively, turn back to heat exchange ice chest 10, in this process, be used for cooling off Sweet natural gas and high pressure nitrogen through in heat exchange ice chest 30, heat exchange ice chest 20 and the heat exchange ice chest 10.After this strand nitrogen after heat exchange heats up in the heat exchange ice chest 10 enters the 603 elementary compressions of decompressor supercharging blower, be cooled to 20 ℃ by water cooler 604, be compressed to 8MPa by nitrogen compressor 605 and nitrogen compressor 607 successively then, correspondence is cooled to 20 ℃ by water cooler 606 and water cooler 608 after every grade of compression, returns heat exchange ice chest 10 by mixing tank 609 at last.
Entering the low-pressure nitrogen that heat exchange ice chest 20 backflowed through another strand nitrogen of nitrogen splitter 601 continues to be chilled to-65 ℃ in advance, enter the low-pressure nitrogen that heat exchange ice chest 30 backflowed then and continue to be cooled to-85 ℃, expand through nitrogen expansion machine 610 again, and to decompressor supercharging blower 611 output mechanical works, pressure is reduced to 1.4MPa, temperature is reduced to-156 ℃, at last successively by heat exchange ice chest 40, heat exchange ice chest 30, heat exchange ice chest 20, turn back to heat exchange ice chest 10, in this process, can be used for cooling heat transferring ice chest 40, heat exchange ice chest 30, the Sweet natural gas and the high pressure nitrogen of process in heat exchange ice chest 20 and the heat exchange ice chest 10.In the heat exchange ice chest 10, heat exchange is warming up to after this strand nitrogen after 17 ℃ enters the 611 elementary compressions of decompressor supercharging blower, be cooled to 20 ℃ through water cooler 612, be compressed to 8MPa through nitrogen compressor 613 and nitrogen compressor 615 successively then, correspondence is cooled to 20 ℃ by water cooler 614 and water cooler 616 after every grade of compression, is back to heat exchange ice chest 10 by mixing tank 609 at last.
Above-mentionedly be back to two strands of nitrogen of heat exchange ice chest 10, after the carbonic acid gas by the carbon dioxide precooling recycle system 50 is pre-chilled to-50 ℃ in advance once more, proceed above-mentioned working cycle by mixing tank 609.
Natural qi exhaustion heavy hydrocarbon and liquefaction system 70 comprise the separator 701 that is connected with heat exchange ice chest 10, the output terminal of separator 701 is divided into two pipelines, article one, pipeline directly connects rectifying tower 702 middle parts, and another connects rectifying tower 702 tops and mixing tank 704 by heat exchange ice chest 20, separator 703 successively;
The top of rectifying tower 702 is connected mixing tank 704 with separator 703, and the output terminal of mixing tank 704 connects heat exchange ice chest 30, heat exchange ice chest 40, Sweet natural gas throttling valve 705 and LNG surge tank 706 successively, and the output terminal of LNG surge tank 706 connects LNG storage tank 707.
The bottom of rectifying tower 702 throttling valve 708, water cooler 709 and LPG (liquefied petroleum gas (LPG), the Liquefied Petroleum Gas) surge tank 710 that is connected in series successively, the output terminal of LPG surge tank 710 connects LPG storage tank 711.
The workflow of natural qi exhaustion heavy hydrocarbon and liquefaction system 70 is, Sweet natural gas by the seabed extraction at first passes through pre-treatment, remove silt wherein, water, sour gas, mercury, behind the impurity such as benzene, enter heat exchange ice chest 10, carbon dioxide precooling in the natural gas via carbon dioxide precooling recycle system 50 is after-50 ℃, enter separator 701 and carry out flash trapping stage, isolated liquid phase directly enters rectifying tower 702, middle part charging as rectifying tower 702, after isolated gas phase enters heat exchange ice chest 20 and is cooled to-65 ℃ by the nitrogen that backflows, enter separator 703 and carry out secondary and separate.
Separator 703 isolated liquid phases enter rectifying tower 702, as its top feed of rectifying tower 702; Separator 703 isolated gas phases after mixing, mixing tank 704 are entered heat exchange ice chest 30 and heat exchange ice chest 40 successively with the top products of rectifying tower 702, be cooled to-151 ℃ by the nitrogen that backflows, make it all liquefaction and cold excessively, be cooled to-159 ℃ through 705 throttlings of Sweet natural gas throttling valve again, wherein about 7% liquid gasification, gas-liquid mixture enters LNG surge tank 706, entering LNG storage tank 707 through LNG surge tank 706 isolated liquid phases stores, after isolated gas phase is discharged from abhiseca, can be used as the low-temperature receiver of Sweet natural gas method of cooling dehydration, can be used as the resurgent gases on absorption tower in the pretreatment system after the re-heat, enter the use that acts as a fuel or generate electricity of fuel gas pipe network at last.
The bottoms of rectifying tower 702 is depressurized to 1.0MPa through throttling valve 708, ℃ enter LPG surge tank 710 through water cooler 709 heat exchange to 35 then, can be used as fuel through LPG surge tank 710 isolated gases uses, isolated liquid phase enters LPG storage tank 711, LPG product in the LPG storage tank 711 contains the above component of more C5, and needing further to handle through land based installation could be as qualified product.
In conjunction with the liquefaction flow path of Sweet natural gas shown in Figure 1, the utility model device can be divided into four modules, is respectively heat exchange ice chest module, heavy hydrocarbon separation module, hydrodynamic force module and product stock module.
As shown in Figure 2, in the heat exchange ice chest module, above-mentioned four heat exchange ice chests 10,20,30,40 are encapsulated in an attemperator the inside, this attemperator connects carbonic acid gas throttling valve 505, Sweet natural gas throttling valve 705 and nitrogen splitter 601.
Wherein, the pipeline 801～802 that is connected with heat exchange ice chest 10, the pipeline 803～804 that is connected with heat exchange ice chest 20, be respectively Sweet natural gas as the liquefaction process of thermal source in the heat exchange ice chest with the pipeline 805～806 that heat exchange ice chest 30 is connected with heat exchange ice chest 40, wherein, Sweet natural gas throttling valve 705 is arranged on the pipeline 806.
The pipeline that is connected with heat exchange ice chest 10 807～808 for after the carbon dioxide coolant throttling as the process of low-temperature receiver precooling Sweet natural gas and nitrogen gas refrigerant in heat exchange ice chest 10, throttling valve 505 is arranged on the pipeline 807.
The nitrogen gas refrigerant of the pipeline that is connected with heat exchange ice chest 10,20,30 809～810 after for compression as thermal source in the heat exchange ice chest by the process of precooling, it is provided with nitrogen splitter 601; The pipeline 813～814 that the pipeline 811～812 that is connected with heat exchange ice chest 10,20,30,40 is connected with heat exchange ice chest 10,20,30 is the process of the nitrogen gas refrigerant after expanding as low-temperature receiver cooled natural gas and high pressure nitrogen refrigeration agent.
As shown in Figure 3, the heavy hydrocarbon separation module comprises 701,703, one mixing tanks 704 of two separators and a rectifying tower 702.Wherein, the pipeline 802 that connects separator 701 is the Sweet natural gases after 10 precoolings of heat exchange ice chest, pipeline 803 the other ends that connect separator 701 gas phase output terminals connect the heat exchange ice chest 20 of heat exchange ice chest module, and the pipeline the other end that connects separator 701 liquid phase output terminals connects rectifying tower 702.The pipeline 804 that connects separator 703 is through heat exchange ice chest 20 cooled Sweet natural gases from heat exchange ice chest module, pipeline 805 the other ends that connect separator 703 gas phase output terminals connect the heat exchange ice chest 30 of heat exchange ice chest module, and the pipeline the other end that connects separator 703 liquid phase output terminals connects rectifying tower 702.The pipeline 815 of rectifying tower 702 bottoms connects the water cooler 708 of product stock module.
As shown in Figure 4, the hydrodynamic force module comprises two nitrogen expansion machines 602,610, two carbon dioxide compressors 501,503, four nitrogen compressors 605,607,613,615,603,611, eight water coolers 502,504,604,606,608,612,614,616 of two decompressor supercharging blowers.
The pipeline 816～813 that connects nitrogen expansion machine 602, and the pipeline 810～811 of connection nitrogen expansion machine 610 is the nitrogen expansion process.The pipeline 814～817 that connects decompressor supercharging blower 603, nitrogen compressor 605,607, and the pipeline 812～818 that connects decompressor supercharging blower 611, nitrogen compressor 613,615 is the nitrogen pressure compression process.The pipeline 808～807 that connects carbon dioxide compressor 501,503 is the carbonic acid gas compression process.
As shown in Figure 5, the product stock module comprises LNG surge tank 706, LNG storage tank 707, LPG surge tank 710, LPG storage tank 711, water cooler 709.Pipeline 806 the other ends that are connected with LNG surge tank 706 connect the Sweet natural gas throttling valve 705 of heat exchange ice chest module, and the pipeline 819 that is connected with LNG surge tank 706 is natural gas liquids (LNG) flash steam; Pipeline 815 the other ends that are connected with LPG surge tank 710 by water cooler 709 connect the throttling valve 708 of heavy hydrocarbon separation module, and the pipeline 820 that connects LPG surge tank 710 is liquefied petroleum gas (LPG) (LPG) flash steam.
In the foregoing description, the used water coolant of all water coolers all is seawater.
Liquifying method of the present utility model may further comprise the steps:
1) will be from the Sweet natural gas of seabed extraction through being input to the heat exchange ice chest after the pre-treatment:
2) after the compressed machine of carbon dioxide that presets in the carbon dioxide precooling recycle system is pressurized to 6MPa, be cooled to 20 ℃ by water cooler, until whole liquefaction, liquid carbon dioxide is depressurized to 0.6MPa through throttling valve again, be cooled to-52 ℃, become gas-liquid two-phase, be used for Sweet natural gas and the high pressure nitrogen imported in the precool heat exchanger ice chest;
3) after the nitrogen that presets in the dinitrogen gas swell refrigeration recycle system is compressed to 8MPa, become high pressure nitrogen input heat exchange ice chest, high pressure nitrogen by carbon dioxide precooling after-50 ℃, be divided into two strands through splitter, one directly expands through the nitrogen expansion machine, and pressure is reduced to 2MPa, and temperature is reduced to-115 ℃; Another strand continues to be chilled to-85 ℃ in advance by the low-pressure nitrogen in the flow back into heat exchange ice chest, expands through the nitrogen expansion machine then, and pressure is reduced to 1.4MPa, and temperature is reduced to-156 ℃; Above-mentioned two strands of low-pressure nitrogen flow back into heat exchange ice chests after overexpansion are used for cooling off high pressure nitrogen and Sweet natural gas, and make natural gas liquefaction, cold excessively; Two strands of nitrogen after heat exchange heats up are through decompressor supercharging blower and a plurality of nitrogen compressor, and stage compression is back to the heat exchange ice chest to 8MPa and by after the water cooler cooling, continues by carbon dioxide precooling;
4) after pretreated Sweet natural gas is pre-chilled to-50 ℃ by the carbon dioxide in the heat exchange ice chest, enter the heavy hydrocarbon separating unit, in the heavy hydrocarbon separating unit, the nitrogen that Sweet natural gas is backflowed progressively cools off, and utilize two gas-liquid separators and a rectifying tower to realize removing of heavy hydrocarbon, removing Sweet natural gas behind the heavy hydrocarbon is cooled to-151 ℃ earlier and makes it all liquefaction and cold excessively, be cooled to-159 ℃ through the throttling valve throttling again, wherein about 7% liquid gasification, gas-liquid mixture enters the LNG surge tank, liquid phase enters the LNG storage tank stores, and gas phase is discharged from the buffering abhiseca and collected.
The various embodiments described above only are used to illustrate the utility model; wherein the structure of each parts, mode of connection, quantity etc. be set all can change to some extent; every equivalents of carrying out on the basis of technical solutions of the utility model and improvement all should not got rid of outside protection domain of the present utility model.
Claims (1)
1. marine natural gas liquefaction device, it is characterized in that: it comprises a heat exchange ice chest, No. two heat exchange ice chests, No. three heat exchange ice chests and No. four heat exchange ice chests, the one cover carbon dioxide precooling recycle system, a cover dinitrogen gas swell refrigeration recycle system and a natural qi exhaustion heavy hydrocarbon of cover and a liquefaction system;
The described carbon dioxide precooling recycle system comprises carbon dioxide compressor, water cooler and the carbonic acid gas throttling valve that connects a described heat exchange ice chest successively, and the output terminal of described carbonic acid gas throttling valve connects a described heat exchange ice chest;
The described dinitrogen gas swell refrigeration recycle system comprises the nitrogen splitter that is connected with a described heat exchange ice chest, and described nitrogen splitter output terminal is divided into two pipelines:
Article one, pipeline directly connects the nitrogen expansion machine, and described nitrogen expansion machine connects a decompressor supercharging blower, and the output terminal of described nitrogen expansion machine connects described No. three heat exchange ice chests, No. two heat exchange ice chests and a heat exchange ice chest successively;
Another pipeline be connected in series successively described No. two heat exchange ice chests, No. three heat exchange ice chests and another nitrogen expansion machine, this described nitrogen expansion machine also connects a decompressor supercharging blower, and the output terminal of this described nitrogen expansion machine connects described No. four heat exchange ice chests, No. three heat exchange ice chests, No. two heat exchange ice chests and a heat exchange ice chest successively;
The input terminus of two described decompressor supercharging blowers all connects a described heat exchange ice chest, and output terminal all be connected in series successively water cooler, nitrogen compressor, water cooler, mixing tank connect a described heat exchange ice chest at last;
Described natural qi exhaustion heavy hydrocarbon and liquefaction system comprise the primary separator that is connected with a described heat exchange ice chest, the output terminal of described primary separator is divided into two pipelines, article one, pipeline directly connects the rectifying tower middle part, and another connects described rectifying tower top by described No. two heat exchange ice chests, second-stage separators successively;
The top of described rectifying tower is connected described No. three heat exchange ice chests, No. four heat exchange ice chests, Sweet natural gas throttling valve and LNG surge tanks with described second-stage separator successively by a mixing tank, and the output terminal of described LNG surge tank connects the LNG storage tank;
The bottom of described rectifying tower be connected in series successively throttling valve, water cooler and LPG surge tank, the output terminal of described LPG surge tank connects the LPG storage tank.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011200190563U CN202030720U (en) | 2011-01-20 | 2011-01-20 | Offshore natural gas liquefaction device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011200190563U CN202030720U (en) | 2011-01-20 | 2011-01-20 | Offshore natural gas liquefaction device |
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| CN202030720U true CN202030720U (en) | 2011-11-09 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104930815A (en) * | 2015-06-16 | 2015-09-23 | 上海交通大学 | Marine natural gas liquefaction and NGL recycling system and application |
| CN106642986A (en) * | 2016-07-15 | 2017-05-10 | 上海利策科技股份有限公司 | Natural gas liquefaction device used for offshore platform |
| CN109297256A (en) * | 2018-11-03 | 2019-02-01 | 中科瑞奥能源科技股份有限公司 | The technique and system of liquid nitrogen gasification preparing liquefied natural gas |
-
2011
- 2011-01-20 CN CN2011200190563U patent/CN202030720U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104930815A (en) * | 2015-06-16 | 2015-09-23 | 上海交通大学 | Marine natural gas liquefaction and NGL recycling system and application |
| CN106642986A (en) * | 2016-07-15 | 2017-05-10 | 上海利策科技股份有限公司 | Natural gas liquefaction device used for offshore platform |
| CN109297256A (en) * | 2018-11-03 | 2019-02-01 | 中科瑞奥能源科技股份有限公司 | The technique and system of liquid nitrogen gasification preparing liquefied natural gas |
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Address after: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Patentee after: China National Offshore Oil Corporation Patentee after: CNOOC Research Institute Patentee after: China Petroleum University (East China) Address before: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Patentee before: China National Offshore Oil Corporation Patentee before: CNOOC Research Center Patentee before: China Petroleum University (East China) |
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| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Co-patentee after: CNOOC research institute limited liability company Patentee after: China Offshore Oil Group Co., Ltd. Co-patentee after: China Petroleum University (East China) Address before: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Co-patentee before: CNOOC Research Institute Patentee before: China National Offshore Oil Corporation Co-patentee before: China Petroleum University (East China) |
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| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20111109 |